US9353040B2 - Method and device for the hydroformylation of isobutene and for the separation of the product mixture - Google Patents

Method and device for the hydroformylation of isobutene and for the separation of the product mixture Download PDF

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US9353040B2
US9353040B2 US14/380,647 US201314380647A US9353040B2 US 9353040 B2 US9353040 B2 US 9353040B2 US 201314380647 A US201314380647 A US 201314380647A US 9353040 B2 US9353040 B2 US 9353040B2
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nanofiltration
methylbutanoic acid
nanofiltration device
concentration
transition metal
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US20150018576A1 (en
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Goetz Baumgarten
Michael Graβ
Alfred Kaizik
Markus Winterberg
Hans-Gerd Lueken
Bart Hamers
Markus Priske
Dirk Fridag
Robert Franke
Dieter Hess
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Evonik Operations GmbH
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/027—Nanofiltration
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/49—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide
    • C07C45/50—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide by oxo-reactions
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/49—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide
    • C07C45/50—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide by oxo-reactions
    • C07C45/505—Asymmetric hydroformylation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/78—Separation; Purification; Stabilisation; Use of additives
    • C07C45/786—Separation; Purification; Stabilisation; Use of additives by membrane separation process, e.g. pervaporation, perstraction, reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/78—Separation; Purification; Stabilisation; Use of additives
    • C07C45/81—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
    • C07C45/82—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C47/00—Compounds having —CHO groups
    • C07C47/02—Saturated compounds having —CHO groups bound to acyclic carbon atoms or to hydrogen
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/23—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups
    • C07C51/235—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups of —CHO groups or primary alcohol groups
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives
    • C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation

Definitions

  • the present invention relates to a process for preparing a product mixture by industrial hydroformylation of an isobutene-containing hydrocarbon stream and for separating the resulting product mixture, and to an apparatus for the process according to the invention and to the use of an inventive apparatus.
  • Hydroformylation is generally understood in the industrial sector to mean the reaction of an olefin with synthesis gas (gas mixture consisting principally of carbon monoxide and hydrogen), usually under pressure and in the presence of a transition metal complex catalyst, to give an aldehyde extended by one carbon atom compared to the olefin.
  • synthesis gas gas mixture consisting principally of carbon monoxide and hydrogen
  • hydroformylation serves to prepare higher aldehydes.
  • Higher aldehydes especially those having 3 to 25 carbon atoms, are utilized, for example, as synthesis precursors for preparation of carboxylic acids and as fragrances. They are often converted industrially by catalytic hydrogenation to the corresponding alcohols, which serve in turn for the production of plasticizers and detergents. Owing to the significance of the hydroformylation products for major industry, the oxo process is performed on the industrial scale.
  • organophosphorus metal complex catalysts based on cobalt or rhodium are nowadays used.
  • the catalysts are dissolved homogeneously in the liquid hydroformylation mixture.
  • the homogeneous catalyst also has to be removed gently from the hydroformylation mixture, since the complex catalyst is comparatively sensitive to changes in state and could lose its activity.
  • the catalyst is separated by distillation from the hydroformylation mixture.
  • EP1931472B1 too is concerned generally with organophilic nanofiltration for separation of homogeneously dissolved catalyst complexes from hydroformylation mixtures.
  • the catalyzed hydroformylation of olefins to the corresponding aldehydes is effected typically in homogeneous liquid phase, which means that catalyst, olefin and products are in one phase, the transition metal complex catalyst being dissolved homogeneously in the liquid reaction mixture which also comprises the olefin to be hydroformylated and products of the hydroformylation.
  • Products formed in the hydroformylation are, as well as said aldehyde, 3-methylbutanal, as the primary product, typically also higher-boiling conversion products (typically referred to as high boilers).
  • an inert solvent for the transition metal complex catalyst for example dioctyl phthalate or diisononyl phthalate or isononyl benzoate or mixtures thereof, may be present in the reaction mixture.
  • High boilers are understood here to mean substances which boil at a higher temperature and have higher molar masses than the primary hydroformylation product (aldehyde having one carbon atom more than the olefin used) and the alcohol obtained therefrom by hydrogenation. High boilers form through conversion reactions from the primary hydroformylation product.
  • the high boilers typically formed in industrial hydroformylations include aldolization products and acetalization products, and also esters which form through reaction of alcohols and acids, the alcohols and acids being formed particularly through disproportionation of aldehydes.
  • the industrial hydroformylation of isobutene typically gives rise to a product mixture which, as well as the primary 3-methylbutanal product which is the target product of the industrial hydroformylation of isobutene, comprises conversion products in the form of high boilers and the transition metal complex catalyst and the free ligands thereof.
  • the product mixture withdrawn from the reactor may also comprise unconverted reactant, i.e. isobutene, hydrogen or carbon monoxide.
  • unconverted reactant i.e. isobutene, hydrogen or carbon monoxide.
  • a process for enriching a homogeneous catalyst from a process stream is known from WO02010097376A1.
  • the process stream originates, for example, from a process for hydroformylation of olefins, preferably having 2 to 25 carbon atoms, to the corresponding aldehydes, especially isononanal and isotridecanal.
  • the homogeneous catalyst from the process stream is enriched by conducting the process stream through at least one nanofiltration membrane consisting entirely or partly of a polymer having planar polymer units joined to one another via a rigid linker, the linker having an internal twist such that at least one planar polymer unit is bonded via the linker in a non-coplanar arrangement with at least one second planar polymer unit.
  • the catalyst system remains in the retentate, while the high boilers are removed with the permeate.
  • the separation by membrane filtration is preferably preceded by a distillative separation of the output from the hydroformylation reactor into a distillate comprising unconverted olefins and the desired aldehydes, and a bottom product comprising high boilers and the catalyst system.
  • Another process for separating and partly recycling a transition metal complex catalyst from a reaction mixture for example from the reaction mixture obtained in an industrial hydroformylation, is known from WO2010097428.
  • This process is based on a combination of an at least one-stage membrane separation and an adsorption. This involves separating a catalyst-containing stream by means of at least one one-stage membrane separation step into a transition metal complex catalyst-enriched retentate stream and a transition metal complex catalyst-depleted permeate stream. The transition metal complex catalyst-enriched retentate stream is recycled into the reactor. The transition metal complex catalyst-depleted permeate stream is sent to an adsorption step in which further separation of the transition metal complex catalyst from the permeate stream is affected.
  • the aim of these and other processes known from the prior art is to separate the transition metal complex catalyst as far as possible from the high boilers in order to achieve maximum recovery of the transition metal complex catalyst.
  • the catalyst removed can—optionally after required workup—be recycled into the hydroformylation reactor, such that the economic viability of the process can be improved.
  • the problem addressed by the present invention is thus that of specifying a process and an apparatus for preparation of a product mixture by industrial hydroformylation of an isobutene-containing hydrocarbon stream and for separation of the resulting product mixture, which enable minimization of the proportion of high boilers in the product mixture and hence enhancement of the yield of the reaction.
  • the aldol condensate can be reduced by reaction with the primary 3-methylbutanal product to give a dihydric C 10 -alcohol, the primary 3-methylbutanal product being oxidized to 3-methylbutanoic acid:
  • the C 15 and C 20 high boilers are formed to a crucial degree substantially via reactions involving 3-methylbutanoic acid.
  • 3-Methylbutanoic acid is occasionally abbreviated hereinafter to 3 MBAc.
  • the inventive solution to the above-mentioned problem of minimizing the proportion of high boilers in the resulting product mixture of the hydroformylation primarily involves separating 3-methylbutanoic acid very substantially from the transition metal complex catalyst to be recycled into the hydroformylation reactor. This can be achieved by, in the step of separating the resulting product mixture from the hydroformylation, enriching the transition metal complex catalyst which is to be recycled into the hydroformylation reactor in the resulting retentate of the nanofiltration device, while the conversion products of the hydroformylation reaction, especially 3 MBAc, are enriched in the resulting permeate of the nanofiltration device.
  • nanofiltration i.e. separation of the resulting product mixture of the hydroformylation using one or more nanofiltration membranes.
  • a nanofiltration device comprising one or more nanofiltration membranes is used, this featuring a particularly low retention for 3-methylbutanoic acid.
  • the retention of the nanofiltration membrane for 3-methylbutanoic acid is preferably ⁇ 1 or less, more preferably ⁇ 5 or less and especially preferably ⁇ 10 or less. The definition of the retention of a membrane can be found further down.
  • the 3-methylbutanoic acid discharged with the permeate of the nanofiltration device is no longer available in the reactor as a reactant for high boiler formation, and so important reactions involved in high boiler formation proceed only to a lower degree, if at all.
  • the loss is reduced based on the primary 3-methylbutanal product.
  • An important aspect of the inventive teaching thus consists in the use of a nanofiltration device for separation of the catalyst complex from the product mixture, this having a particularly high permeability for 3-methylbutanoic acid.
  • a “nanofiltration device” in the context of this invention is understood to mean a separation apparatus which accomplishes its separation task exclusively with the aid of membranes, at least one of the membranes being a nanofiltration membrane.
  • the nanofiltration device may comprise one or more membrane separation stages; accordingly, the nanofiltration device may work in one or more stages.
  • Each membrane separation stage has three connections, a feed and two outlets, namely retentate and permeate.
  • the constituents of the feed which pass through the membrane accumulate in the permeate, while the substances which are retained by the membrane accumulate in the retentate.
  • the resulting permeate and the resulting retentate are understood to mean the two outputs of a nanofiltration device at the interfaces thereof with the other components of the apparatus for performance of the process according to the invention. If the nanofiltration device works with only one stage, and therefore has only one membrane separation stage, the resulting permeate or the resulting retentate of the nanofiltration device corresponds to the permeate or the retentate of the sole membrane separation
  • Nanofiltration is a pressure-driven membrane separation process.
  • the separation limit molecular weight cut-off, MWCO; cf. Y. H. See Toh, X. X. Loh, A. Bismarck, A. G. Livingston, In search of a standard method for the characterisation of organic solvent nanofiltration membranes, J. Membr. Sci, 291 (2007)120-1251) is in the range from 150 g/mol to 2000 g/mol.
  • the separation limit is defined as the molar mass of a preferably inert indicator system (for example polystyrene standards or alkane standards in Toh, Loh, Bismarck and Livingston) at which a membrane has a retention of 90%.
  • the exact separation limit of a nanofiltration membrane is determined by the membrane used and the respective solvent, and by the process conditions such as pressure and temperature. In nanofiltration, impervious or porous membranes are used. Nanofiltration membranes feature low retention for low molecular weight organic substances.
  • the retention R of a membrane is determined by the local concentrations of a component i of the non-permeating stream (retentate) and of the stream permeating through the membrane (permeate). If retentate and permeate have ideal mixing along the membrane, the local retentate and permeate concentrations correspond to the respective concentrations of the retentate and permeate obtained overall.
  • c Pi is the concentration of component i in the permeate P and c Ri is the concentration of component i in the retentate R.
  • c Pi >c Ri , and R ⁇ 0.
  • the nanofiltration device for use in the process according to the invention comprises one or more nanofiltration membranes, the or at least one of the nanofiltration membranes having a retention for 3-methylbutanoic acid of ⁇ 1 or less, more preferably ⁇ 5 or less and especially ⁇ 10 or less.
  • a retention for 3-methylbutanoic acid of ⁇ 1 or less, more preferably ⁇ 5 or less and especially ⁇ 10 or less.
  • Membranes which appear suitable for the separation task are those which have a separation-active layer of a material selected from cellulose acetate, cellulose triacetate, cellulose nitrate, regenerated cellulose, polyimides, polyamides, polyetheretherketones, sulphonated polyetheretherketones, aromatic polyamides, polyamidimides, polybenzimidazoles, polybenzimidazolones, polyacrylonitrile, polyarylethersulphones, polyesters, polycarbonates, polytetrafluoroethylene, polyvinylidene fluoride, polypropylene, polydimethylsiloxane, silicones, polyphosphazenes, polyphenylsulphides, polybenzimidazoles, nylon-6,6, polysulphones, polyanilines, polyurethanes, acrylonitrile/glycidyl methacrylate (PANGMA), polytrimethylsilylpropyne, polymethylpentyne, polyvinyltrimethylsi
  • PIM intrinsic microporosity
  • membranes which have, as the separation-active layer, a polymer layer of polydimethylsiloxane, polyimide, polyamidimide, acrylonitrile/glycidyl methacrylate (PANGMA), polyamide or polyetheretherketone, which are formed from polymers with intrinsic microporosity (PIM) such as PIM-1, or wherein the separation-active layer is formed by means of a hydrophobized ceramic membrane.
  • PIM intrinsic microporosity
  • membranes composed of silicones or polyamidimide. Such membranes are commercially available.
  • nanofiltration membranes comprising one or more polymers containing imide groups or consisting of one or more polymers containing imide groups are particularly suitable for the discharge of 3-methylbutanoic acid from the product mixture of the hydroformylation which is supplied as feed to the nanofiltration device.
  • Representatives of this membrane class are especially membranes of polyimide or polyamidimide.
  • thermoplastic polyimide which is obtainable under the Matrimid® brand name from Huntsman Advanced Materials GmbH, Basel (Switzerland).
  • Nanofiltration membranes composed of polyimide or polyamidimide feature particularly low retention for 3-methylbutanoic acid.
  • Nanofiltration membranes comprising or consisting of one or more polymers containing imide groups, the polymer(s) containing imide groups being selected such that the retention of the nanofiltration membrane for 3-methylbutanoic acid is ⁇ 1 or less, preferably ⁇ 5 or less and more preferably ⁇ 10 or less.
  • Nanofiltration membranes containing imide groups are commercially available, for example under the STARMEM® 122 and 240 product names from W. R. Grace & Co.-Conn. 7500 Grace Drive Columbia, Md. 21044 US, or membranes of the Puramem® and Duramem® product families obtainable from Evonik Industries AG, Essen (Germany). Puramem® and Duramem® contain polyimides such as P84 and/or Matrimid 5218.
  • the nanofiltration device for use in the process according to the invention more preferably comprises one or more nanofiltration membranes, the or at least one of the nanofiltration membranes having a separation limit in the range from 150 to 2000 g/mol, preferably 200 to 600 g/mol, more preferably 350 to 500. Since retention of 3-methylbutanoic acid is unwanted in the process according to the invention, preference is given in accordance with the invention to using a nanofiltration membrane whose separation limit is higher than the molar mass of 3-methylbutanoic acid (102 g/mol). Since the high boilers are not to be retained in the retentate either, the separation limit thereof is preferably above the molar mass of the high boilers (200 to 350 g/mol) but below that of the catalyst (500 to 1000 g/mol).
  • nanofiltration membranes comprising or consisting of one or more polymers containing imide groups, the polymer(s) containing imide groups being selected such that the separation limit of the nanofiltration membrane is in the range from 150 to 2000 g/mol.
  • the step of separation of the product mixture obtained by hydroformylating the isobutenic hydrocarbon stream in the nanofiltration device is preferably performed
  • the resulting reaction mixture leaving the hydroformylation reactor is preferably first cooled, if necessary for reasons of membrane stability or for the establishment of the separation limit, and decompressed, preferably to a pressure exceeding 200 kPa.
  • volatile constituents such as unconverted isobutene or hydrogen and carbon monoxide are partly removed and optionally recycled.
  • the synthesis gas which remains under the decompression pressure is used to supply the product mixture comprising the primary 3-methylbutanal product, conversion products in the form of high boilers and 3-methylbutanoic acid and the transition metal complex catalyst and the free ligands thereof and any unconverted product to a high-pressure membrane pump which generates the transmembrane pressure needed for the nanofiltration process.
  • the high-pressure pump may be proceeded upstream by a preliminary filter system.
  • the transmembrane pressure is understood to mean the pressure difference between the feed side and the permeate side of the nanofiltration membrane per separation stage. This pressure difference is the primary driving force of the membrane filtration.
  • the nanofiltration device may comprise a multitude of separation stages in the form of membrane modules (connected in series or parallel), the respective permeate obtained after each separation stage being supplied as feed to the next separation stage, and the permeate from the last separation stage being supplied to the thermal separation.
  • Each separation stage comprises at least one membrane module, each membrane module comprising an individual or more than one nanofiltration membrane.
  • a membrane module is understood by the person skilled in the art to mean a practically manageable use-specific arrangement of the membrane in an assembly.
  • the step of thermal separation of the permeate typically comprises a distillation or thin-film evaporator or falling-film evaporator or a combination thereof, in which the first fraction is obtained as the top product and the second fraction as the bottom product.
  • the step of thermal separation no further separation of the second fraction from the thermal separation by means of a nanofiltration device is required.
  • a further separation of the second fraction obtained as the bottom product is dispensable especially when the transition metal complex catalyst is already retained in the retentate in the prior separation of the product mixture which is the result of the hydroformylation in the nanofiltration device to such a high degree that only such a small amount of catalyst is present in the permeate that the cost and inconvenience of recovery from the high-boiling (second) fraction of the thermal separation is uneconomic.
  • reaction mixture is understood to mean the overall mixture present in the hydroformylation reactor comprising the reactants (isobutene and synthesis gas), the primary product of the hydroformylation (3-methylbutanal), conversion products formed therefrom (3-methylbutanoic acid and high boilers) and the transition metal complex catalyst.
  • unconverted reactants are not separated from the reactor output upstream of the nanofiltration device, these are part of the product mixture which has been run into the feed of the nanofiltration device.
  • full conversion of the isobutene is desirable, but cannot always be achieved in industrial practice. Typical conversion rates exceed 95% by weight.
  • Unconverted isobutene may be removed immediately upstream of the nanofiltration device in order that the feed thereof is virtually isobutene-free.
  • This variant is preferable since thermal separation processes damage the catalyst complex.
  • the carbon monoxide reactant should, however, preferably also be present in the feed, permeate and retentate of the nanofiltration device in order to stabilize the catalyst complex.
  • one or more process parameters in the step of hydroformylating the isobutenic hydrocarbon stream are set such that the total concentration of conversion products in the form of high boilers and 3-methylbutanoic acid, based on the weight of the product mixture, i.e. the reactor output, is 30% by weight or less, the parameter(s) to be set preferably being selected from the group consisting of pressure, temperature, mean residence time of the reaction mixture in the hydroformylation reactor, composition of the synthesis gas, concentration of the transition metal and transition metal-ligand ratio of the transition metal complex catalyst.
  • a reduction in the mean residence time of the reaction mixture in the hydroformylation reactor makes it possible to reduce the time available for the unwanted conversion reactions, but the mean residence time, on the other hand, must be sufficiently high to allow an economically viable degree of conversion of the reactants.
  • the mean residence time can be influenced, for example, by the design of the length of the reactor.
  • a reduction in the temperature in the hydroformylation reactor can reduce the rate of the unwanted conversion reactions, but the temperature, on the other hand, must be sufficiently high to allow an economically viable degree of conversion of the reactants.
  • the concentration of the catalyst complex in the resulting permeate is preferably 0.03% by weight or less.
  • the step of hydroformylating the isobutenic hydrocarbon stream is preferably performed
  • transition metal complex catalyst whose transition metal is rhodium and/or whose ligand(s) is/are selected from the group of the organophosphorus ligands. It is also possible to use a transition metal complex catalyst whose transition metal is cobalt.
  • a preferred process according to the invention comprises the steps of
  • Suitable methods for monitoring the concentration of 3-methylbutanoic acid in the retentate of the nanofiltration device, and preferably also in the resulting product mixture of the hydroformylation and/or in the feed and/or in the permeate of the nanofiltration device comprise a measurement of the concentration of 3-methylbutanoic acid in the respective process stream with a measurement method selected from the group consisting of gas chromatography.
  • a rise in the concentration of 3-methylbutanoic acid in the retentate of the nanofiltration device could indicate blockage of the nanofiltration membrane by deposits (membrane fouling).
  • the recycling of the retentate into the hydroformylation reactor is stopped. This prevents the concentration of 3-methylbutanoic acid from rising in the hydroformylation reactor, thus promoting the unwanted formation of high boilers.
  • exceedance of a fixed maximum concentration of 3-methylbutanoic acid in the retentate of the nanofiltration device additionally initiates a check of the function of the nanofiltration device and, if necessary, an exchange or regeneration of one or more nanofiltration membranes.
  • a measure could be appropriate especially if the likewise monitored concentration of 3-methylbutanoic acid in the permeate simultaneously falls below a particular minimum value (see below).
  • a sudden rise in the concentration of 3-methylbutanoic acid in the feed of the nanofiltration device could even be an indication of failure or out-of-control regulation of one or more process parameters in the hydroformylation.
  • this described variant of the process according to the invention can contribute to reliable monitoring of the process parameters of the hydroformylation, and may even contribute to avoidance of incorrect production and disrupted operation.
  • one or more process parameters in the step of hydroformylating the isobutenic hydrocarbon stream in the hydroformylation reactor are modified such that the concentration of 3-methylbutanoic acid in the feed of the nanofiltration device is lowered to or below the fixed maximum.
  • the suitable setting of one or more process parameters of the hydroformylation is preferably effected as described above, the parameters to be set being selected especially from the group consisting of pressure, temperature, mean residence time of the reaction mixture in the hydroformylation reactor, composition of the synthesis gas, concentration of the transition metal and transition metal/ligand ratio of the transition metal complex catalyst.
  • a process according to the invention for preparing a product mixture by industrial hydroformylation of an isobutene-containing hydrocarbon stream and for separation of the resulting product mixture individual or all features of the developments and variants emphasized above as particularly preferred are combined with one another, in order to achieve an optimal separation of 3-methylbutanoic acid from the transition metal complex catalyst to be recycled into the reactor and low formation of 3-methylbutanoic acid and high boilers in the hydroformylation and comprehensive monitoring of the concentration of 3-methylbutanoic acid in all relevant streams in the process according to the invention.
  • the present invention relates additionally to an apparatus for the performance of the process according to the invention, especially for the above-described preferred variants of the process according to the invention.
  • An apparatus for performance of the process according to the invention comprises:
  • the apparatus for performance of the process according to the invention may also comprise constituents customary in the prior art, for example pumps, customary metering, measurement, control and regulation devices, heating and cooling apparatuses etc.
  • constituents customary in the prior art for example pumps, customary metering, measurement, control and regulation devices, heating and cooling apparatuses etc.
  • Such constituents of apparatuses for industrial synthesis and separation processes are known to those skilled in the art, these constituents forming part of the prior art and being customary in chemical process technology.
  • the hydroformylation reactor used is preferably an apparatus from the group consisting of stirred tank, bubble column, jet nozzle reactor, tubular reactor and loop reactor, and the apparatus may be provided with internals.
  • the hydroformylation reactor takes the form of a bubble column reactor.
  • the length dimension of the hydroformylation reactor is preferably selected so as to result in a residence time of the reaction mixture in the hydroformylation reactor which is sufficient for an economically viable degree of conversion of the reactants to the primary 3-methylbutanal hydroformylation product but does not allow the high degree of conversion of the primary 3-methylbutanal hydroformylation product to conversion products in the form of 3-methylbutanoic acid and high boilers.
  • the nanofiltration device of the inventive apparatus preferably comprises one or more membrane modules.
  • the nanofiltration membranes are arranged such that the flow over the retentate side of the nanofiltration membrane may be such as to counteract the concentration polarization of the components removed, i.e. of the transition metal complex catalyst, and also to impose the necessary driving force (pressure).
  • the permeate is combined in the permeate collecting space on the permeate side of the nanofiltration membrane and removed from the module.
  • Standard membrane modules have the nanofiltration membranes in the form of membrane disks, membrane pads or membrane pockets.
  • membrane modules with open-channel pad module systems in which the nanofiltration membranes are thermally welded or bonded to form membrane pockets or pads, or wound modules in which the nanofiltration membranes are bonded or welded to form membrane pockets or membrane pads and are wound with feed spacers around a permeate collecting tube.
  • the nanofiltration device of the inventive apparatus is configured such that the above-described preferred process parameters, especially process parameters from the group consisting of pressure, temperature, mean residence time of the reaction mixture in the hydroformylation reactor, composition of the synthesis gas, concentration of the transition metal and transition metal/ligand ratio of the transition metal complex catalyst, can be established and/or the above-described preferred variants of the execution of the step of separation of the resulting product mixture of the hydroformylation can be implemented.
  • process parameters especially process parameters from the group consisting of pressure, temperature, mean residence time of the reaction mixture in the hydroformylation reactor, composition of the synthesis gas, concentration of the transition metal and transition metal/ligand ratio of the transition metal complex catalyst
  • the nanofiltration device may comprise a multitude of separation stages arranged such that, after each separation stage, the permeate obtained is supplied in each case as feed to the next separation stage, and the permeate from the last separation stage is supplied to the thermal separation.
  • Each separation stage may be designed as a membrane module or several membrane modules arranged in parallel.
  • Each membrane module may comprise one or more nanofiltration membranes arranged in parallel.
  • the nanofiltration device preferably comprises one or more nanofiltration membranes, the or at least one of the nanofiltration membranes having a separation limit in the range from 150 to 2000 g/mol, preferably 200 to 600 g/mol and more preferably from 350 to 500 g/mol.
  • the inventive apparatus additionally comprises
  • the apparatus for determining the concentration of 3-methylbutanoic acid in the feed of the nanofiltration device is preferably selected from the group consisting of gas chromatographs. The same applies to the optional devices for determination of the concentration of 3-methylbutanoic acid in the retentate and/or permeate of the nanofiltration device.
  • apparatuses for taking samples from the resulting product mixture of the hydroformylation, or from the feed and/or retentate and/or permeate of the nanofiltration device may be provided.
  • the concentration of 3-methylbutanoic acid is determined, for example, in a process control laboratory.
  • the present invention further relates to the use of an inventive apparatus, especially in the preferred embodiments thereof, for preparation of a product mixture by industrial hydroformylation of an isobutene-containing hydrocarbon stream and for separation of the resulting product mixture, especially by a process according to one of the preferred variants of the above-described process according to the invention.
  • FIG. 1 apparatus for preparation of a product mixture by industrial hydroformylation of an isobutene-containing hydrocarbon stream and for separation of the resulting product mixture by the process according to the invention
  • FIG. 2 graph of 3 MBAc concentrations in the feed, retentate and permeate of the nanofiltration
  • FIG. 3 graph of the 3 MBAc retention of the nanofiltration.
  • an apparatus shown in FIG. 1 comprising a hydroformylation reactor R in the form of a bubble column, a nanofiltration device M and a distillation device D.
  • sampling devices P which enable samples to be taken at particular intervals from the product stream 2 leaving the reactor R, and also from the retentate 3 and the permeate 4 of the nanofiltration device M.
  • the nanofiltration device M comprises a membrane module in the form of a wound module.
  • the nanofiltration membrane is a membrane of the STARMEM 122 type from W. R. Grace & Co and comprises polyimide P84.
  • the hydroformylation reactor R is supplied with a hydrocarbon stream 1 comprising isobutene and synthesis gas,
  • the isobutene is hydroformylated to 3-methylbutanal at a pressure in the range from 0.2 to 8.0 MPa and a temperature in the range from 70 to 130° C. with a mean residence time in the range from 1 to 4 hours, a synthesis gas composition (CO/H2) of 1:3 to 3:1, a rhodium concentration in the range from 20 to 100 ppm and a rhodium/ligand ratio in the range from 1:4 to 1:50.
  • CO/H2 synthesis gas composition
  • the resulting product mixture 2 of the hydroformylation in which the concentration of 3-methylbutanoic acid is in the range between 0.01 and 0.04% by weight, is subsequently separated in a nanofiltration device M at a temperature in the range from 30 to 35° C., a transmembrane pressure in the range from 3.1 to 3.8 MPa and a partial carbon monoxide pressure in the range from 0.9 to 1.2 MPa.
  • the nanofiltration device M is designed such that the Reynolds number is between 170 and 900 in the course of flow over the nanofiltration membrane.
  • a resulting retentate 3 and a resulting permeate 4 are withdrawn from the nanofiltration device M.
  • the ratio of product mixture 2 supplied to the membrane—also referred to as feed—and permeate 4 was set to 0.82.
  • the retentate stream 3 in which the transition metal complex catalyst is enriched is recycled into the reactor R.
  • Samples are taken with sampling apparatuses P at regular intervals from the product mixture 2 leaving the reactor R, the retentate 3 and the permeate 4 , in order to determine the concentration of 3-methylbutanoic acid in the respective stream.
  • the resulting permeate 4 of the nanofiltration device M in which the primary 3-methylbutanal hydroformylation product and 3-methylbutanoic acid are enriched, is separated by means of distillation in a thermal separation device in the form of a distillation plant D into a first fraction 5 and a second fraction 6 .
  • the concentration of 3-methylbutanal is higher than in the second fraction 6
  • the concentration of 3-methylbutanoic acid and high boilers is lower than in the second fraction.
  • FIG. 2 shows the 3 MBAc concentration in the feed, retentate and permeate of the nanofiltration M over a period of 500 hours.
  • FIG. 3 shows distinctly negative retentions of the Starmem 122 membrane used for the 3-MBAc in the nanofiltration step. The retention is defined as 1 ⁇ (permeate concentration)/(retentate concentration).

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US20150018576A1 (en) 2015-01-15
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